CN103409232B - Production method of safflower seed oil - Google Patents
Production method of safflower seed oil Download PDFInfo
- Publication number
- CN103409232B CN103409232B CN201310349918.2A CN201310349918A CN103409232B CN 103409232 B CN103409232 B CN 103409232B CN 201310349918 A CN201310349918 A CN 201310349918A CN 103409232 B CN103409232 B CN 103409232B
- Authority
- CN
- China
- Prior art keywords
- oil
- flos carthami
- temperature
- water
- technical process
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
Landscapes
- Fats And Perfumes (AREA)
Abstract
The invention provides a production method of safflower seed oil. A raw material of safflower seed oil is subjected to a technical process comprising pretreatment, leaching and refining to obtain the safflower seed oil product. Compared with the prior art, the invention has the beneficial effect that the process employs subcritical low temperature leaching at a temperature below 50 DEG C; and the cake contains 0.5-1.0% of residual oil. The method increases oil extraction rate and product yield, reduces production cost and increases economic income.
Description
Technical field
The present invention relates to a kind of working method of food, particularly the production method of a kind of safflower oil.
Background technology
Safflower is also named Flos Carthami, chrysanthemum safflower, FLOS CARTHAMI from Henan of China, Flos Carthami and Flos Carthami, for the herbaceous plant of composite family, Linoleic Acid in Safflower Oil content up to 78%-85%, linolic acid be unique a kind of human body must and the lipid acid that self can not synthesize voluntarily in body, must by meal service, it can reduce cholesterol levels, reduce the chance of cholesterol deposits on atherosclerotic plaque, thus effectively prevent hyperlipidemia, arteriosclerosis and coronary heart disease.Have very high pharmaceutical use, the preparation technology of traditional safflower oil is milling process, and make the oil of more than 10% remain in grouts, not only cause waste, same production cost also remains high always.
Summary of the invention
The present invention proposes the production method of a kind of safflower oil, solve deficiency of the prior art, this technique adopts subcritical low-temp extraction, temperature is below 50 degree, and the Residual oil in grouts is 0.5-1.0%, improves the yield of oil yield and product, reduce production cost, improve economic return.
Technical scheme of the present invention is achieved in that the production method of a kind of safflower oil, and it take Semen Flos Carthami as raw material, successively through the technical process of pre-treatment, leaching, refining, obtains safflower oil.
One, pre-treatment:
(1) remove the impurity in Semen Flos Carthami, described impurity has dust, stone, metal and other impurity;
(2) by removing impurity after Semen Flos Carthami carry out fragmentation, isolate safflower benevolence, safflower benevolence made thickness at 0.1-0.5mm embryo sheet, embryo sheet after drying moisture control≤8.0%.
Leaching thickness needed for operation and moisture content requirement to reach, preparing for leaching operation; Pre-treatment is operation very crucial together, and it directly affects the oil yield of leaching and the height of dregs of rice material residua content, so the blank of making from pre-treatment wants thickness moderate, moisture content is suitable for, and has certain toughness.
Concrete technical process is: Semen Flos Carthami → just clear → deironing → de-stone → fragmentation → separation of hull from kernel → safflower benevolence → soften → roll embryo → drying.
A, just clear: to adopt air blast process, as China
rural areawith " wind scoop ", by the principle that the rice shell of having rolled over separates, be placed in by Semen Flos Carthami on wind scoop, control the continuous down freely falling body of a certain amount of Semen Flos Carthami, turn over the wind of one certain speed in its vertical side south, the dust, impurity etc. lighter than Semen Flos Carthami are blown away.
B, deironing: the metallic impurity in deironing apparatus removing Semen Flos Carthami;
C, de-stone: remove the stone in Semen Flos Carthami through gravity grading stone remover;
D, fragmentation: through the broken Semen Flos Carthami of rubber roll husker.
E, separation of hull from kernel: make broken Semen Flos Carthami separation of hull from kernel through kernel husk separator, do not have broken Semen Flos Carthami to get back to again rubber roll husker again broken.
F, softening: safflower benevolence is steamed through cooking pot and fried, and temperature controls at 35-45 DEG C, makes safflower benevolence by thermal softening.
G, roll embryo: crushing roll is bundled into blank thickness at 0.1-0.5mm, embryo tablet quality: thickness evenly, flexible, without pasty state;
H, drying:
1. the portion of water in Semen Flos Carthami blank mainly removed by drying machine, to reach the index leached needed for operation.
2. principle of work: after material enters material holding chamber, under chain drives, refractory slab evenly moves forward.Through the warm air of interchanger heating, under the effect of blower fan, then air compartment is through refractory slab, penetrates material, and the moisture in material is taken out of.
3. operational requirement: by suitably regulating the handwheel of stepless speed changer, will carry out the rotating speed of regulation output wheel, to reach the travelling speed (material is generally about 7 minutes from material holding chamber to the time of discharging) regulating material.
The temperature of dried material controls at 60-80 DEG C.
The height of material on refractory slab is regulated by controlling level setter, and controlling level is generally 10-15cm.Material level is too thin, and hot blast will " short circuit "; Material level is too thick, and hot blast can not pass material, and do not reach the drying effect removing moisture, the moisture controlled of embryo sheet is ≤8%.
The process flow of leaching is entered after the assay was approved through dried Semen Flos Carthami embryo sheet.
Two, leach:
By the embryo sheet of gained after pretreatment technology flow process with normal butane mixing, the inlet amount of embryo sheet joins in batch extractor by the 55-70% of batch extractor volume, normal butane exceeds the high computational of 100-150mm by the position of embryo sheet in batch extractor, extraction temperature is≤50 DEG C, extraction time is 25-35min, then carry out precipitation, discharge, after extract technology flow process, obtain Semen Flos Carthami crude oil.
The production principle of a, leaching: the characteristic that grease and normal butane can dissolve mutually, and the feature that normal butane is in a liquid state under the pressure of certain temperature.
B, charging: with the fastest speed charging, every tank embryo sheet inlet amount of batch extractor wants consistent, embryo sheet inlet amount is the 55-70% of batch extractor volume, and its measure is the position determined according to practical experience, at the end of charging is fast, rotate and reverse one, two circles, hocket, embryo sheet is uniformly distributed in batch extractor, if window does not see, then fine rotation paddle, in order to avoid paddle gear draws light.
C, emptying: when the charging of embryo sheet is complete, to start to start emptying vacuum pump, not abnormal, then open exhaust-valve and vacuumize, till reaching-0.07-1Mpa, valve-off again.
D, leaching: inject normal butane to batch extractor from solvent storage tank, when entering solvent to regulation liquid level, until exceed embryo sheet charge level 100-150mm, opening to stir positive and negatively stirs, once every positive and negative stirring in 10 minutes, be beneficial to oil extraction, controlling batch extractor service pressure is below 0.6Mpa later, in tank, temperature is below 50 DEG C, and extraction time is 25-35 minute.
E, filtration: after leaching terminates, start from this tank to temporary storage tank suction filtration mixing oil:
(1), before suction filtration mixing oil, the outlet valve (be generally and often open) of solvent pump must be opened, otherwise solvent pump top hole pressure is too high, causes pump to damage.During operation, jockey valve turn on pump behind the door, generally first closes pump during shutdown, rear closing valve.
(2), during suction filtration, can not significantly stir back and forth, to affect infiltration.Can stir 1/4 week every ten minutes positive and negative alternates, too thick to avoid filter cake to tie layer.
(3), suction filtration fast at the end of (now batch extractor internal pressure is lower than normally leaching pressure), open batch extractor and temporary storage tank or evaporating pot top equilibration tube, two pressure tanks balanced.When the concentrated blend extracted out enters evaporating pot, the pressure of tank inside can be reduced by starting compressor, solvent pump outlet system pressure being reduced, is beneficial to suction filtration.
(4), circulating leaching four times successively.Suction filtration of trying one's best is clean, is conducive to thus reducing dregs of rice Residual oil.
(5), heavy in mixing oil temporary storage tank and compressor outlet surge tank in slag, each is all over when leaching (before entering mixing oil after evacuation), in the bits suction tank in above-mentioned tank.Open large valve during deslagging, precipitation slag can be got rid of totally.
F, at the end of batch extractor mixing oil suction filtration, close batch extractor mixing oil outlet valve, open precipitation pipeline valve, start compressor, start precipitation.Intermittent stirring during precipitation, and heat gradually.When batch extractor pressure close to zero time, restart precipitation vacuum pump, help precipitation.When batch extractor pressure reaches 0.08Mpa, stop precipitation, close whole desolventizing system.
Precaution:
(1), the order of each valve opening and requirement: the precipitation valve first opening batch extractor top, starts spray pump.Then starting compressor, slowly opening valve (when just starting precipitation, the pressure in batch extractor is too high, makes intake pressure Tai Gaotai fast, affects the work-ing life of compressor), when the pressure in batch extractor is close to standard-sized sheet compressor air intake valve during 0.2Mpa.
(2), stir problem: when precipitation just starts, rush to stir; When precipitation is after about ten minutes, start to stir, rotating periodical operation during stirring, and increase all numbers of stirring gradually.
(3), heating problems: when precipitation just starts, not instant heating, but along with the reduction of pressure increase vapor pressure gradually.As the close-0.04Mpa of pressure, steam off valve, stops heating.
(4), discharge: precipitation terminates, and starts to arrange dregs of rice material.First open dregs of rice handling equipment before row's dregs of rice material, then open blanking valve vacuum breaker, start to arrange dregs of rice material; Extractive crudeoil sends into refining procedure, the dregs of rice material warehouse-in after leaching.
Three, refining:
Comprise come unstuck, depickling, washing, decolouring and deodorization technical process:
The object of refining is to remove some the harmful compositions in grease and the storage to grease, to improve the use value of grease, extends storage period.
A, the technical process of coming unstuck are: after extract technology flow process gained Semen Flos Carthami crude oil in add water, the weight ratio of the water Flos Carthami seed crude oil added is 2-4:1, oil temperature is heated to 45-55 DEG C, water temperature is at 55-60 DEG C, water adds in crude oil and stirs 15-30min, then staticly settle 5-7h and isolate colloid, obtain degummed oil.
Remove the operation of colloid in crude oil for coming unstuck, colloidalmaterial in crude oil mainly phosphatide, phosphatide has wetting ability and hydrophobic character, and the former has stronger water-retaining capacity, along with the increase absorbing moisture content, phosphatide volume expands gradually, the mutual sorption of particle forms micelle, and proportion increases, and after water suction, phosphatide polarity increases in addition, in oil, solubleness declines, and can separate from oil.According to these features of phosphatide, aquation method separating phospholipids can be utilized.The object of heating is to react quickening, and reduces the entrainment of grease in phosphatide.
The technical process of b, depickling is:
Containing free fatty acids in crude oil, the process of sloughing these lipid acid is depickling, and with in caustic soda (NaOH) and free fatty acids, generate soap stock in oil, soap stock becomes undissolved jelly and precipitates.It is to be noted that in caustic soda and while free fatty acids, the saponification of grease also may be there is, cause the increase of refining consumption.Therefore want strict red-tape operati condition to obtain the finished product of high quality and high yield.
For the acidic component in effectively and in degummed oil, make the processed oil good mouthfeel processed, the acid value value of degummed oil need be detected, accurately to calculate required amount of adding alkali, method of calculation: the acid value of degummed oil after testing, in NaOH, draws the acid value value of degummed oil.Add the weight of weight=(the acid value value+0.3 of degummed oil) g/kg × Semen Flos Carthami crude oil of sodium hydroxide.Then the sodium hydroxide of this weight is mixed with the sodium hydroxide solution of 10%.
It is draw according to a large amount of experimental datas and actual derivation of production that above-mentioned calculating adds drawing of the formula of sodium hydroxide weight, can be used in production reality.
Degummed oil is warming up to 55-65 DEG C, then while stir with the rotating speed of 55-65 rev/min, while add sodium hydroxide solution, during state separated to the neat soap in fluid, stir with the rotating speed of 25-35 rev/min and heat to 65-75 DEG C, to soap stock be clamminess and be lasting suspended state time, stop heating, keep oil liquid temperature at about 65-75 DEG C, when proportion increase is sunk rapidly after continuing with the rotating speed of 25-35 rev/min stirring, neat soap to be absorbed water, leave standstill 7-9 hour, remove soap stock.
The technical process of c, washing is: the oil through alkali-refining deacidification will add certain hot wash, washes out soap stock residual in oil.
Oily mixing speed after deacidifying process is controlled at 15-30 rev/min, heat to 70-75 DEG C and stop heating, by adding equably in oil higher than the hot water of oil temperature 5-10 DEG C of heating in advance, each washing water consumption is the 5-10% of weight of oil, do not add water also too not soon or too slow, to add equably, after adding water, continue to stir 15-20 minute, stirring is stopped to staticly settle, under the condition that scheduling of production allows, sedimentation time will be grown as far as possible, general 3-4h, then discharge water, to note first quick and back slow when discharging water, when sewage occurs, slow down the speed of discharging water, oil is prevented to enter out, discharge water when seeing oil, stopping discharges water.
The technical process of d, decolouring is: the oil after washing process flow process, acid value controls at 1.0(in KOH) below, then enter in Decolouring pot and carry out intensification heating, add gac when temperature rises to 65-85 DEG C, the add-on of gac is the 2-6% of weight of oil, then with the speed warming while stirring of 55-65 rev/min, reach 105-110 DEG C to oil temperature and stop heating, decolour when being incubated 20-30 minute, is then cooled to 70-75 DEG C, filters.
The method that the measuring method of above-mentioned acid value adopts the mensuration of GB/T5530-2005 vegetable and animals oils acid value to specify is carried out.When acid value is not in 1.0, can add concentration is that the sodium hydroxide solution of 10-25% controls.
The technical process of e, deodorization is: after the oil after decoloration process flow process enters odor removing pot, open heat conductive oil inlet valve to heat, utilize thermal oil that oil temperature is raised to 145-150 DEG C, oil in odor removing pot is made fully to stir continuation heat temperature raising, when temperature is raised to 210-240 DEG C, carries out being incubated through high temperature deodorization in 3-5 hour, namely complete deodorization procedures, by oil cooling to about 20-30 DEG C, obtain finished product safflower oil.
Compared with prior art, the invention has the beneficial effects as follows:
(1) this technique adopts subcritical low-temp extraction, and temperature is below 50 degree, and the Residual oil in grouts is 0.5-1.0%, improves oil yield, and oil yield improves 4-8% compared with pressed oil; The yield making product last also improves 4-10%.
(2) owing to also improving the yield of product while improve oil yield, namely improve economic return greatly; Under the condition utilizing less raw material, obtain the finished product safflower oil of equal value, namely saved raw materials cost, reduced production cost.
Embodiment
Be clearly and completely described the technical scheme in the present invention below, obviously, described embodiment is only several embodiments wherein of the present invention, instead of whole embodiments.Based on the embodiment in the present invention, those of ordinary skill in the art, not making the every other embodiment obtained under creative work prerequisite, belong to the scope of protection of the invention.
Embodiment 1:
A production method for safflower oil, it for raw material, successively through the technical process of pre-treatment, leaching, refining, obtains safflower oil with 1000Kg Semen Flos Carthami.
One, pre-treatment:
(1) remove the impurity in Semen Flos Carthami, described impurity has dust, stone, metal and other impurity;
(2) by removing impurity after Semen Flos Carthami carry out fragmentation, isolate safflower benevolence, safflower benevolence made thickness at 0.2mm embryo sheet, embryo sheet after drying moisture control≤8.0%.
Concrete technical process is: Semen Flos Carthami → just clear → deironing → de-stone → fragmentation → separation of hull from kernel → safflower benevolence → soften → roll embryo → drying.
A, just clear: to adopt air blast process, as China
rural areawith " wind scoop ", by the principle that the rice shell of having rolled over separates, be placed in by Semen Flos Carthami on wind scoop, control the continuous down freely falling body of a certain amount of Semen Flos Carthami, turn over the wind of one certain speed in its vertical side south, the dust, impurity etc. lighter than Semen Flos Carthami are blown away.
B, deironing: the metallic impurity in deironing apparatus removing Semen Flos Carthami;
C, de-stone: remove the stone in Semen Flos Carthami through gravity grading stone remover;
D, fragmentation: through the broken Semen Flos Carthami of rubber roll husker.
E, separation of hull from kernel: make broken Semen Flos Carthami separation of hull from kernel through kernel husk separator, do not have broken Semen Flos Carthami to get back to again rubber roll husker again broken.
F, softening: safflower benevolence is steamed through cooking pot and fried, and temperature controls at 40 DEG C, makes safflower benevolence by thermal softening.
G, roll embryo: crushing roll is bundled into blank thickness at 0.2mm, embryo tablet quality: thickness evenly, flexible, without pasty state;
H, drying:
The height of material on refractory slab is 12cm, and drying temperature is 65 DEG C, and material is 7 minutes from material holding chamber to the time of discharging.The moisture controlled of embryo sheet is ≤8.0%.
The process flow of leaching is entered after the assay was approved through dried Semen Flos Carthami embryo sheet.
Two, leach:
By the embryo sheet of gained after pretreatment technology flow process with normal butane mixing, the inlet amount of embryo sheet joins in batch extractor by 65% of batch extractor volume, normal butane exceeds the high computational of 120mm by the position of embryo sheet in batch extractor, extraction time is 30min, then carry out precipitation, discharge, after extract technology flow process, obtain Semen Flos Carthami crude oil.
A, charging: with the fastest speed charging, every tank embryo sheet inlet amount of batch extractor wants consistent, embryo sheet inlet amount is 65% of batch extractor volume, and its measure is the position determined according to practical experience, at the end of charging is fast, rotate and reverse one, two circles, hocket, embryo sheet is uniformly distributed in batch extractor, if window does not see, then fine rotation paddle, in order to avoid paddle gear draws light.
B, emptying: when the charging of embryo sheet is complete, to start to start emptying vacuum pump, not abnormal, then open exhaust-valve and vacuumize, till reaching-0.05Mpa, valve-off again.
C, leaching: inject normal butane to batch extractor from solvent storage tank, when entering solvent to regulation liquid level, until exceed embryo sheet charge level 120mm, opening to stir positive and negatively stirs, once every positive and negative stirring in 10 minutes, be beneficial to oil extraction, controlling batch extractor service pressure is 0.5Mpa later, in tank, temperature is at 45 DEG C, and extraction time is 30 minutes.
D, filtration: after leaching terminates, start from this tank to temporary storage tank suction filtration mixing oil:
Extractive crudeoil 165.3kg sends into refining procedure, and oil yield is 16.53%, the dregs of rice material warehouse-in after leaching.
Three, refining:
Comprise come unstuck, depickling, washing, decolouring and deodorization technical process:
The object of refining is to remove some the harmful compositions in grease and the storage to grease, to improve the use value of grease, extends storage period.
A, the technical process of coming unstuck are: after extract technology flow process gained Semen Flos Carthami crude oil in add water, the weight ratio of the water Flos Carthami seed crude oil added is 3:1, the add-on of water is 495.9kg, oil temperature is heated to 50 DEG C, water temperature is at 56 DEG C, water adds in crude oil and stirs 20min, then staticly settles 6h and isolates colloid, obtain degummed oil.
The technical process of b, depickling is:
After testing, in NaOH, the acid value value of this degummed oil is 3.0g/kg to the acid value of degummed oil.The weight adding sodium hydroxide is the weight 165.3kg=545.49g of (3.0+0.3) g/kg × Semen Flos Carthami crude oil.Then the sodium hydroxide of this weight is mixed with the sodium hydroxide solution of 10%.
Degummed oil is warming up to 60 DEG C, then while stir with the rotating speed of 60 revs/min, while add the sodium hydroxide solution of above-mentioned configuration, during state separated to the neat soap in fluid, stir with the rotating speed of 30 revs/min and heat to 70 DEG C, to soap stock be clamminess and be lasting suspended state time, stop heating, keep oil liquid temperature at 70 DEG C, when proportion increase is sunk rapidly after continuing with the rotating speed of 30 revs/min stirring, neat soap to be absorbed water, leave standstill 8 hours, remove soap stock.
The technical process of c, washing is: the oil through alkali-refining deacidification will add certain hot wash, washes out soap stock residual in oil.
Oily mixing speed after deacidifying process is controlled at 15 revs/min, heat to 72 DEG C and stop heating, the hot water higher than oil temperature 8 DEG C heated in advance is added in oil equably, each washing water consumption is 7% of weight of oil, do not add water also too not soon or too slow, to add equably, after adding water, continue stirring 18 minutes, stirring is stopped to staticly settle 3.5h, under the condition that scheduling of production allows, sedimentation time can be grown as far as possible, then discharge water, to note first quick and back slow when discharging water, when sewage occurs, slow down the speed of discharging water, oil is prevented to enter out, discharge water when seeing oil, stopping discharges water.
The technical process of d, decolouring is: the oil after washing process flow process, acid value controls at 1.0(in KOH) below, then enter in Decolouring pot and carry out intensification heating, add gac when temperature rises to 75 DEG C, the add-on of gac is 4% of weight of oil, then with the speed warming while stirring of 60 revs/min, reach 107 DEG C to oil temperature and stop heating, when being incubated, decolouring 25 minutes, is then cooled to 73 DEG C, filters.
The technical process of e, deodorization is: after the oil after decoloration process flow process enters odor removing pot, open heat conductive oil inlet valve to heat, utilize thermal oil that oil temperature is raised to 150 DEG C, make oil in odor removing pot fully stir continuation heat temperature raising, when temperature is raised to 220 DEG C, carry out being incubated through high temperature deodorization in 4 hours, namely deodorization procedures is completed, by oil cooling to 25 DEG C, obtain finished product safflower oil 133.4kg, yield is 13.34%.
Embodiment 2:
A production method for safflower oil, it for raw material, successively through the technical process of pre-treatment, leaching, refining, obtains safflower oil with 1000Kg Semen Flos Carthami.
One, pre-treatment:
(1) remove the impurity in Semen Flos Carthami, described impurity has dust, stone, metal and other impurity; ,
(2) by removing impurity after Semen Flos Carthami carry out fragmentation, isolate safflower benevolence, safflower benevolence made thickness at 0.5mm embryo sheet, embryo sheet after drying moisture control≤8.0%.
Concrete technical process is: Semen Flos Carthami → just clear → deironing → de-stone → fragmentation → separation of hull from kernel → safflower benevolence → soften → roll embryo → drying.
A, just clear: to adopt air blast process, as China
rural areawith " wind scoop ", by the principle that the rice shell of having rolled over separates, be placed in by Semen Flos Carthami on wind scoop, control the continuous down freely falling body of a certain amount of Semen Flos Carthami, turn over the wind of one certain speed in its vertical side south, the dust, impurity etc. lighter than Semen Flos Carthami are blown away.
B, deironing: the metallic impurity in deironing apparatus removing Semen Flos Carthami;
C, de-stone: remove the stone in Semen Flos Carthami through gravity grading stone remover;
D, fragmentation: through the broken Semen Flos Carthami of rubber roll husker.
E, separation of hull from kernel: make broken Semen Flos Carthami separation of hull from kernel through kernel husk separator, do not have broken Semen Flos Carthami to get back to again rubber roll husker again broken.
F, softening: safflower benevolence is steamed through cooking pot and fried, and temperature controls at 45 DEG C, makes safflower benevolence by thermal softening.
G, roll embryo: crushing roll is bundled into blank thickness at 0.5mm, embryo tablet quality: thickness evenly, flexible, without pasty state;
H, drying:
The height of material on refractory slab is 15cm, and drying temperature is 70 DEG C, and material is 9 minutes from material holding chamber to the time of discharging.The moisture controlled of embryo sheet is ≤8.0%.
The process flow of leaching is entered after the assay was approved through dried Semen Flos Carthami embryo sheet.
Two, leach:
By the embryo sheet of gained after pretreatment technology flow process with normal butane mixing, the inlet amount of embryo sheet joins in batch extractor by 58% of batch extractor volume, normal butane exceeds the high computational of 145mm by the position of embryo sheet in batch extractor, extraction time is 35min, then carry out precipitation, discharge, after extract technology flow process, obtain Semen Flos Carthami crude oil.
A, charging: with the fastest speed charging, every tank embryo sheet inlet amount of batch extractor wants consistent, embryo sheet inlet amount is 58% of batch extractor volume, and its measure is the position determined according to practical experience, at the end of charging is fast, rotate and reverse one, two circles, hocket, embryo sheet is uniformly distributed in batch extractor, if window does not see, then fine rotation paddle, in order to avoid paddle gear draws light.
B, emptying: when the charging of embryo sheet is complete, to start to start emptying vacuum pump, not abnormal, then open exhaust-valve and vacuumize, till reaching 0.5Mpa, valve-off again.
C, leaching: inject normal butane to batch extractor from solvent storage tank, when entering solvent to regulation liquid level, until exceed embryo sheet charge level 145mm, opening to stir positive and negatively stirs, once every positive and negative stirring in 10 minutes, be beneficial to oil extraction, controlling batch extractor service pressure is 0.4Mpa later, in tank, temperature is at 43 DEG C, and extraction time is 35 minutes.
D, filtration: after leaching terminates, start from this tank to temporary storage tank suction filtration mixing oil:
Extractive crudeoil 167.8kg sends into refining procedure, and oil yield is 16.78%, the dregs of rice material warehouse-in after leaching.
Three, refining:
Comprise come unstuck, depickling, washing, decolouring and deodorization technical process:
The object of refining is to remove some the harmful compositions in grease and the storage to grease, to improve the use value of grease, extends storage period.
A, the technical process of coming unstuck are: after extract technology flow process gained Semen Flos Carthami crude oil in add water, the weight ratio of the water Flos Carthami seed crude oil added is 2:1, the add-on of water is, 335.6kg, oil temperature is heated to 45 DEG C, and water temperature is at 58 DEG C, and water adds in crude oil and stirs 25min, then staticly settle 5h and isolate colloid, obtain degummed oil.
The technical process of b, depickling is:
After testing, in NaOH, the acid value value of this degummed oil is 3.1g/kg to the acid value of degummed oil.The weight adding sodium hydroxide is the weight 167.8kg=570.52g of (3.1+0.3) g/kg × Semen Flos Carthami crude oil.Then the sodium hydroxide of this weight is mixed with the sodium hydroxide solution of 10%.
Degummed oil is warming up to 65 DEG C, then while stir with the rotating speed of 65 revs/min, while add the sodium hydroxide solution of above-mentioned configuration, during state separated to the neat soap in fluid, stir with the rotating speed of 35 revs/min and heat to 70 DEG C, to soap stock be clamminess and be lasting suspended state time, stop heating, keep oil liquid temperature at 65 DEG C, when proportion increase is sunk rapidly after continuing with the rotating speed of 30 revs/min stirring, neat soap to be absorbed water, leave standstill 7 hours, remove soap stock.
The technical process of c, washing is: the oil through alkali-refining deacidification will add certain hot wash, washes out soap stock residual in oil.
Oily mixing speed after deacidifying process is controlled at 25 revs/min, heat to 75 DEG C and stop heating, the hot water higher than oil temperature 10 DEG C heated in advance is added in oil equably, each washing water consumption is 6% of weight of oil, do not add water also too not soon or too slow, to add equably, after adding water, continue stirring 20 minutes, stirring is stopped to staticly settle 4h, under the condition that scheduling of production allows, sedimentation time can be grown as far as possible, then discharge water, to note first quick and back slow when discharging water, when sewage occurs, slow down the speed of discharging water, oil is prevented to enter out, discharge water when seeing oil, stopping discharges water.
The technical process of d, decolouring is: the oil after washing process flow process, acid value controls at 1.0(in KOH) below, then enter in Decolouring pot and carry out intensification heating, add gac when temperature rises to 68 DEG C, the add-on of gac is 6% of weight of oil, then with the speed warming while stirring of 65 revs/min, reach 110 DEG C to oil temperature and stop heating, when being incubated, decolouring 30 minutes, is then cooled to 75 DEG C, filters.
The technical process of e, deodorization is: after the oil after decoloration process flow process enters odor removing pot, open heat conductive oil inlet valve to heat, utilize thermal oil that oil temperature is raised to 150 DEG C, make oil in odor removing pot fully stir continuation heat temperature raising, when temperature is raised to 210 DEG C, carry out being incubated through high temperature deodorization in 5 hours, namely deodorization procedures is completed, by oil cooling to 30 DEG C, obtain finished product safflower oil 135.7kg, yield is 13.57%.
Embodiment 3:
A production method for safflower oil, it for raw material, successively through the technical process of pre-treatment, leaching, refining, obtains safflower oil with 1000Kg Semen Flos Carthami.
One, pre-treatment:
(1) remove the impurity in Semen Flos Carthami, described impurity has dust, stone, metal and other impurity;
(2) by removing impurity after Semen Flos Carthami carry out fragmentation, isolate safflower benevolence, safflower benevolence made thickness at 0.3mm embryo sheet, embryo sheet after drying moisture control≤8.0%.
Concrete technical process is: Semen Flos Carthami → just clear → deironing → de-stone → fragmentation → separation of hull from kernel → safflower benevolence → soften → roll embryo → drying.
A, just clear: to adopt air blast process, as China
rural areawith " wind scoop ", by the principle that the rice shell of having rolled over separates, be placed in by Semen Flos Carthami on wind scoop, control the continuous down freely falling body of a certain amount of Semen Flos Carthami, turn over the wind of one certain speed in its vertical side south, the dust, impurity etc. lighter than Semen Flos Carthami are blown away.
B, deironing: the metallic impurity in deironing apparatus removing Semen Flos Carthami;
C, de-stone: remove the stone in Semen Flos Carthami through gravity grading stone remover;
D, fragmentation: through the broken Semen Flos Carthami of rubber roll husker.
E, separation of hull from kernel: make broken Semen Flos Carthami separation of hull from kernel through kernel husk separator, do not have broken Semen Flos Carthami to get back to again rubber roll husker again broken.
F, softening: safflower benevolence is steamed through cooking pot and fried, and temperature controls at 45 DEG C, makes safflower benevolence by thermal softening.
G, roll embryo: crushing roll is bundled into blank thickness at 0.3mm, embryo tablet quality: thickness evenly, flexible, without pasty state;
H, drying:
The height of material on refractory slab is 14cm, and drying temperature is 80 DEG C, and material is 6 minutes from material holding chamber to the time of discharging.The moisture controlled of embryo sheet is ≤8.0%.
The process flow of leaching is entered after the assay was approved through dried Semen Flos Carthami embryo sheet.
Two, leach:
By the embryo sheet of gained after pretreatment technology flow process with normal butane mixing, the inlet amount of embryo sheet joins in batch extractor by 70% of batch extractor volume, normal butane exceeds the high computational of 110mm by the position of embryo sheet in batch extractor, extraction time is 28min, then carry out precipitation, discharge, after extract technology flow process, obtain Semen Flos Carthami crude oil.
A, charging: with the fastest speed charging, every tank embryo sheet inlet amount of batch extractor wants consistent, embryo sheet inlet amount is 68% of batch extractor volume, and its measure is the position determined according to practical experience, at the end of charging is fast, rotate and reverse one, two circles, hocket, embryo sheet is uniformly distributed in batch extractor, if window does not see, then fine rotation paddle, in order to avoid paddle gear draws light.
B, emptying: when the charging of embryo sheet is complete, to start to start emptying vacuum pump, not abnormal, then open exhaust-valve and vacuumize, till reaching 0.8Mpa, valve-off again.
C, leaching: inject normal butane to batch extractor from solvent storage tank, when entering solvent to regulation liquid level, until exceed embryo sheet charge level 110mm, opening to stir positive and negatively stirs, once every positive and negative stirring in 10 minutes, be beneficial to oil extraction, controlling batch extractor service pressure is 0.4Mpa later, in tank, temperature is at 40 DEG C, and extraction time is 28 minutes.
D, filtration: after leaching terminates, start from this tank to temporary storage tank suction filtration mixing oil:
Extractive crudeoil 167.7kg sends into refining procedure, and oil yield is 16.77%, the dregs of rice material warehouse-in after leaching.
Three, refining:
Comprise come unstuck, depickling, washing, decolouring and deodorization technical process:
The object of refining is to remove some the harmful compositions in grease and the storage to grease, to improve the use value of grease, extends storage period.
A, the technical process of coming unstuck are: after extract technology flow process gained Semen Flos Carthami crude oil in add water, the weight ratio of the water Flos Carthami seed crude oil added is 4:1, the add-on of water is 670.8kg, oil temperature is heated to 55 DEG C, water temperature is at 60 DEG C, water adds in crude oil and stirs 30min, then staticly settles 5h and isolates colloid, obtain degummed oil.
The technical process of b, depickling is:
After testing, in NaOH, the acid value value of this degummed oil is 3.05g/kg to the acid value of degummed oil.The weight adding sodium hydroxide is the weight 167.7kg=561.795g of (3.05+0.3) g/kg × Semen Flos Carthami crude oil.Then the sodium hydroxide of this weight is mixed with the sodium hydroxide solution of 10%.
Degummed oil is warming up to 55 DEG C, then while stir with the rotating speed of 55 revs/min, while add the sodium hydroxide solution of above-mentioned configuration, during state separated to the neat soap in fluid, stir with the rotating speed of 25 revs/min and heat to 65 DEG C, to soap stock be clamminess and be lasting suspended state time, stop heating, keep oil liquid temperature at 65 DEG C, when proportion increase is sunk rapidly after continuing with the rotating speed of 35 revs/min stirring, neat soap to be absorbed water, leave standstill 9 hours, remove soap stock.
The technical process of c, washing is: the oil through alkali-refining deacidification will add certain hot wash, washes out soap stock residual in oil.
Oily mixing speed after deacidifying process is controlled at 30 revs/min, heat to 70 DEG C and stop heating, the hot water higher than oil temperature 6 DEG C heated in advance is added in oil equably, each washing water consumption is 9% of weight of oil, do not add water also too not soon or too slow, to add equably, after adding water, continue stirring 20 minutes, stirring is stopped to staticly settle 3h, under the condition that scheduling of production allows, sedimentation time can be grown as far as possible, then discharge water, to note first quick and back slow when discharging water, when sewage occurs, slow down the speed of discharging water, oil is prevented to enter out, discharge water when seeing oil, stopping discharges water.
The technical process of d, decolouring is: the oil after washing process flow process, acid value controls at 1.0(in KOH) below, then enter in Decolouring pot and carry out intensification heating, add gac when temperature rises to 83 DEG C, the add-on of gac is 6% of weight of oil, then with the speed warming while stirring of 65 revs/min, reach 110 DEG C to oil temperature and stop heating, when being incubated, decolouring 30 minutes, is then cooled to 75 DEG C, filters.
The technical process of e, deodorization is: after the oil after decoloration process flow process enters odor removing pot, open heat conductive oil inlet valve to heat, utilize thermal oil that oil temperature is raised to 148 DEG C, make oil in odor removing pot fully stir continuation heat temperature raising, when temperature is raised to 240 DEG C, carry out being incubated through high temperature deodorization in 3 hours, namely deodorization procedures is completed, by oil cooling to 20 DEG C, obtain finished product safflower oil 136.5kg, yield is 13.65%.
The foregoing is only preferred embodiment of the present invention, not in order to limit the present invention, within the spirit and principles in the present invention all, any amendment done, equivalent replacement, improvement etc., all should be included within protection scope of the present invention.
Claims (2)
1. a production method for safflower oil, is characterized in that: it take Semen Flos Carthami as raw material, successively through the technical process of pre-treatment, leaching, refining, obtains Semen Flos Carthami processed oil;
The technical process of described refining comprise come unstuck, depickling, washing, decolouring and deodorization technical process;
Described technical process of coming unstuck is: after extract technology flow process gained Semen Flos Carthami crude oil in add water, the weight ratio of the water Flos Carthami seed crude oil added is 2-4:1, oil temperature is heated to 45-55 DEG C, water temperature is at 55-60 DEG C, water adds in crude oil and stirs 15-30 minute, then staticly settle 5-7 hour and isolate colloid, obtain degummed oil;
The technical process of described depickling is: degummed oil is warming up to 55-65 DEG C, then while stir with the rotating speed of 55-65 rev/min, while add sodium hydroxide solution, during state separated to the neat soap in fluid, stir with the rotating speed of 25-35 rev/min and heat to 65-75 DEG C, to soap stock be clamminess and be lasting suspended state time, stop heating, keep oil liquid temperature at 65-75 DEG C, when after continuing with the rotating speed of 25-35 rev/min stirring, neat soap to be absorbed water, proportion increase is sunk rapidly, leave standstill 7-9 hour, remove soap stock;
The technical process of described washing is: control at 15-30 rev/min by the oily mixing speed after deacidifying process, heat to 70-75 DEG C and stop heating, by adding equably in oil higher than the hot water of oil temperature 5-10 DEG C of heating in advance, each washing water consumption is the 5%-10% of weight of oil, after adding water, continue to stir 15-20 minute, stop stirring staticly settling 3-4 hour, then water is released;
The technical process of described decolouring is: the oil after washing process flow process, in KOH, acid value controls below 1.0, then enters in Decolouring pot and carries out intensification heating, add gac when temperature rises to 65-85 DEG C, the add-on of gac is the 2-6% of weight of oil, then with the speed warming while stirring of 55-65 rev/min, reach 105-110 DEG C to oil temperature and stop heating, the decolorization operations 20-30 minute when being incubated, then be cooled to 70-75 DEG C, filter;
The technical process of described deodorization is: after the oil after decoloration process flow process enters odor removing pot, oil temperature is raised to 145-150 DEG C, oil in odor removing pot is made fully to stir continuation heat temperature raising, be incubated when temperature is raised to 210-240 DEG C, through deodorization in 3-5 hour, namely complete deodorization procedures, by oil cooling to 20-30 DEG C, obtain finished product safflower oil;
The technical process of described leaching is: by the embryo sheet of gained after pretreatment technology flow process with normal butane mixing, the inlet amount of embryo sheet joins in batch extractor by the 55-70% of batch extractor volume, normal butane exceeds the high computational of 100-150mm by the position of embryo sheet in batch extractor, extraction temperature is≤50 DEG C, extraction time is 25-35 minute, then carry out precipitation, discharge, after extract technology flow process, obtain Semen Flos Carthami crude oil.
2. the production method of a kind of safflower oil according to claim 1, is characterized in that: described pretreated technical process is:
(1) impurity in Semen Flos Carthami is removed,
(2) by removing impurity after Semen Flos Carthami carry out fragmentation, isolate safflower benevolence, safflower benevolence made thickness at 0.1-0.5mm embryo sheet, embryo sheet after drying moisture control≤8.0%.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310349918.2A CN103409232B (en) | 2013-08-13 | 2013-08-13 | Production method of safflower seed oil |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310349918.2A CN103409232B (en) | 2013-08-13 | 2013-08-13 | Production method of safflower seed oil |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103409232A CN103409232A (en) | 2013-11-27 |
| CN103409232B true CN103409232B (en) | 2015-01-21 |
Family
ID=49602275
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201310349918.2A Expired - Fee Related CN103409232B (en) | 2013-08-13 | 2013-08-13 | Production method of safflower seed oil |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103409232B (en) |
Families Citing this family (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103766509A (en) * | 2014-01-03 | 2014-05-07 | 李文华 | Safflower seed oil material suitable for household oil press and preparation method thereof |
| CN103981024B (en) * | 2014-05-06 | 2016-02-03 | 新疆裕民天鼎红花油有限公司 | Safflower oil method of refining |
| CN104212626B (en) * | 2014-08-15 | 2019-08-23 | 南阳泰瑞生物科技股份有限公司 | A method of with subcritical fluid extraction cape jasmine oil |
| CN104450177A (en) * | 2014-11-13 | 2015-03-25 | 江苏金洲粮油食品有限公司 | Physical refining process of safflower seed oil |
| CN105647636A (en) * | 2016-01-20 | 2016-06-08 | 和县绿源油脂有限公司 | Energy-saving type extracted oil technological process with high oil yield |
| CN105969515A (en) * | 2016-07-20 | 2016-09-28 | 许炳初 | Leaching refinement technique of rapeseed oil |
| FI129367B (en) | 2018-12-28 | 2021-12-31 | Neste Oyj | A method for treating lipid materials |
| CN110628502A (en) * | 2019-11-11 | 2019-12-31 | 卫辉市鑫福林卫红花种植专业合作社 | Preparation method of fennel seed oil |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101012409A (en) * | 2007-02-04 | 2007-08-08 | 黄宝生 | Method of fast extracting neem emulsifiable solution |
| CN102586007A (en) * | 2012-03-05 | 2012-07-18 | 湖南湘浩油茶生物科技有限公司 | Method for extracting tea oil |
-
2013
- 2013-08-13 CN CN201310349918.2A patent/CN103409232B/en not_active Expired - Fee Related
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101012409A (en) * | 2007-02-04 | 2007-08-08 | 黄宝生 | Method of fast extracting neem emulsifiable solution |
| CN102586007A (en) * | 2012-03-05 | 2012-07-18 | 湖南湘浩油茶生物科技有限公司 | Method for extracting tea oil |
Non-Patent Citations (5)
| Title |
|---|
| 李新华等.浸出制油的工艺流程及工艺要点.《粮油加工学》.中国农业大学出版社,2009,第210页. * |
| 王丽琼.溶剂浸出法制油技术.《粮油加工技术》.化学工业出版社,2007,第110-112页. * |
| 红花籽油提取工艺的优化研究;陈婵等;《江西农业学报》;20091231;第21卷(第12期);第137页右栏"1.3红花籽油的提取方法" * |
| 红花籽的开发利用;潘涛江;《中国油脂》;20010228;第26卷(第2期);第57-58页 * |
| 赵萍.油脂精炼.《粮油食品工艺》.甘肃科学技术出版社,2004,第258-264页. * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN103409232A (en) | 2013-11-27 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103409232B (en) | Production method of safflower seed oil | |
| CN102550708A (en) | Method for preparing Cyperus esculentus edible oil | |
| CN102226127A (en) | Raw oil refining technique | |
| CN105664523A (en) | Small-size extraction and concentration unit for producing cream formula and extraction and concentration technique thereof | |
| CN104531327B (en) | The environmental friendly regenerated device of waste oil | |
| CN101906129A (en) | Method for separating purified saponin | |
| CN102643611B (en) | High-efficiency energy-saving low-cost high-quality rosin production process and production line equipment | |
| CN1068360A (en) | From oil tea (tea-seed) grouts, extract the technology of tea oil and saponin | |
| CN1667105A (en) | Process for processing tea seed oil | |
| CN212998514U (en) | Be used for glossy ganoderma composition extraction device | |
| CN104206644B (en) | The pea separation protein preparation technology of a kind of improvement | |
| CN107226832A (en) | A kind of new method that chenodeoxycholic acid is prepared by raw material of chicken courage | |
| CN108191730A (en) | A kind of production method that high purity lutein crystal is prepared by marigold extractum | |
| CN110540898A (en) | Tea seed oil finish machining process | |
| CN209974507U (en) | High-speed centrifugal type oil-water separator for impurity-removing bone white soup | |
| CN110591810A (en) | Gardenia oil extraction process | |
| CN108114000A (en) | A kind of method for quickly purifying for preparing liquid preparation raw material donkey-hide gelatin | |
| CN206396110U (en) | A kind of rosin production system of processing | |
| CN109666083B (en) | Plant polysaccharide extraction device and method for extracting bletilla striata polysaccharide by using plant polysaccharide extraction device | |
| CN106699624A (en) | Production method of lutein | |
| CN108042573A (en) | A kind of method that liquid preparation raw material donkey-hide gelatin quickly removes floating | |
| CN206391886U (en) | A kind of energy-efficient knot screen of rosin | |
| CN111876264A (en) | Rapid deacidification and low-sulfur high-yield production system for producing fuel oil by using waste animal and vegetable oil | |
| CN104814244A (en) | Extracting method for high-purity sweet potato protein | |
| CN205205066U (en) | Device for extracting turpentine from middle -layer resin liquid |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20150121 Termination date: 20170813 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |